METHOD AND APPARATUS FOR BIOLOGICAL ACTIVATION WASTE WATER TREATMENT

Abstract: Biological activation waste water purification, wherein the waste water is biologically purified in an activation process, in course of which a nitrification occurred. The activation mixture is brought in the circulation circuit with a plug flow character, while the purified water is taken away from the said circuit and the activation mixture is mixed with the waste water after the purified water was taken away, hereby an oxygen lack at the surface of the particles of the activated sludge is caused bringing denitrification processes about. Resulting mixture is aerated which keeps the activated sludge in suspension and during the plug flow causes a gradual oxygen saturation. The apparatus comprises always two separation spaces (4) arranged adjacent to each other by their longitudinal sides, in which communication connections with the activation space are formed and the longitudinal distribution channel (5) formed between the said longitudinal walls is completely closed by an end wall at one side while at the opposite side a passage is arranged, by means of which it is connected with a system of flow channels (9, 7).

Description: METHOD AND APPARATUS FOR BIOLOGICAL ACTIVATION WASTE WATER TREATMENT The present invention relates to a method for biological activation waste water purification, wherein the waste water is purified in an activation process, during which a nitrification occurs. The present invention also relates to an apparatus for realizing said method, which comprises in a common tank an activation space and upwards extending longitudinal separation spaces, from which the outlets for purified water are led out, where each separation space is defined by the partitions and the faces and communicates with the activation space at one longitudinal side. BACKGROUND OF THE INVENTION An effective protection for the surface water, including seas from eutrophisation requires the utmost effectivity of removal of macrobiogen elements as nitrogen and phosphorus, the presence of which in the waste water is the main cause for the eutrophisation phenomenon. That's why all systems for waste water purification have to consider this call for removing the nitrogen and phosphorus. Hitherto known and used systems for waste water purification with simultaneous reduction of the nitrogen content are orientated to biological processes, which seem to be the most economical ones. All said processes require first a conversion of the oxidable nitrogen forms, i.e. the ammoniacal and organic nitrogen, through the nitrification processes to the nitrate form. Then the nitrate reduction through the denitrification processes to the gaseous nitrogen follows. The nitrification requires a presence of the nitrification bacteria in the activated sludge, which requires a sufficient sludge age, practically the entire nitrification being attained at the sludge age of 30 days, which corresponds to the sludge load 0.12 kg of biological oxygen demand in five days per one kilogramme of volatile suspended solids of the activated sludge multiplied by the number of the days, further called as kg BOD s /kg VSS.d .In addition, the nitrification processes require a sufficient concentration of the dissolved oxygen, as a rule over two milligramme of the oxygen per one liter of the liquid - further called as 2 mg 0 2 /l. The following denitrification is then in progress while there is a shortage of dissolved oxygen in the liquid, whereby the microorganisms get the necessary oxygen through nitrate reduction. The prior art knows three essential alternatives for the solution of the system for complex biological water purification with a simultaneous nitrification and denitrification. The first alternative is an intermittent denitrification. In this solution the nitrification and denitrification phases of the activation purification periodically alternate through an intermittent aerating. The disadvantage of this solution is a reduced effectiveness of the intermittent process compared with the continual one, complicated regulation of the process and also ceasing of the suspension of the activated sludge during the aerating interruption. Another alternative is a preceeding denitrification. In this solution is a separated denitrification in the form of a perfectly mixed tank with an intense mixing supply realized before the aerated activation. During the preceeding denitrification process the waste water is carried out together with the activation mixture recirculated from the aerated activation. The disadvantage of the preceeding denitrification is the necessity to create a separated denitrification activation space with an independent source of movement of the activation mixture in order to secure an activated sludge suspendation. Another disadvantage is that a part of the surface of the denitrification space is not utilized for the activated sludge separation, the not utilized part being up to 25% of the surface in a reactor in a municipal waste water treatment plant. The third known alternative of denitrification during the biological water purification is a denitrification in a circulation circuit of a type with oxidization ditches and carousal systems. In this case the functions of aeration and mixing of the waste water with the activation mixture are fused with supplying the movement of the activation mixture in the purifying system, in one system in the form of a mechanic aerator. With a plug flow of the activation mixture •• through the circulation circuit saturation of the activation mixture with the dissolved oxygen occurs, through that a nitrification occurs and through a gradual consumption of the oxygen by the oxidation processes of the biodegrada ion and nitrification the oxygen content in the activation mixture is decreasing, so that at the end of the circulation circuit the denitrification process is performed with an oxygen lack. Said technical solution of the denitrification shows many disadvantages. Mechanical aeration needs flat, not deep tanks, which need a large construction place. The surface of the tank is not used for separation of the activated sludge, the consequence of which is the requirement of completing of the activation apparatus by an independent separation equipment, which further increases the construction place size necessary and therefore the investment costs. Sideline independent separation with a forced recirculation through the separated sludge settling is not very effective and causes a low operating concentration in the activation part. The need of a low loading of the activated sludge with the sludge age of 30 days results in large volumes of the activation space. A considerable disadvantage of the circulation circuits is also a high sludge index in the activated sludge resulting from an insufficient releasing of the gaseous nitrogen bubbles sticking to activated sludge particles during the the denitrification, which results in a significant lowering of the apparatus capacity. Another disadvantage of the fusing of three functions, i.e. aeration, supplying of movement of the activation mixture and mixing the waste water with the activation mixture, is that said fusing causes lowering of the denitrification effectiveness in the waste water with a higher content of the nitrogen pollution, which results from a lack of a carbon supply needed for denitrification processes in the denitrification part. To provide a sufficiently effective nitrification and denitrification it is therefore necessary to combine said apparatus with an intermittent aeration of the activation mixture with all the negative effects on the intermittent process. The above mentioned known solutions of the denitrification show disadvantages for both new waste water purification plant construction and reconstruction of existing classical waste water purification plants, which no more respond to the increased demands for a purified water quality considering the eutrophisation elements. There is a lot of municipal waste water purification plants built in the fully developed industrial countries which already need to be intensified or reconstructed. Hitherto existing solutions of denitrification are not suitable for it, because they call for either a new waste water purification plant construction or at least considerable building rearrangements in the classical municipal waste water purification plants. That's why an urgent need to create a solution enabling the use of the hitherto existing municipal waste water purification plants, which would at the same time fulfill the contemporary ecological demands, has arisen. The object of present invention is to eliminate as much of the disadvantages of the known solutions as possible and to create a new method and apparatus realizing an essential intensification of biological activation waste water purification also with a possibility to use already existing classical waste water purification plants. SUMMARY OF THE INVENTION The subject matter of the method according to the invention is that the activation mixture is brought into the circulation circuit with a plug flow character, wherefrom the purified water is taken away by a fluidized bed filtration and the activation mixture is afterwards mixed with raw waste water, which causes an oxygen lack at the surface of the particles of the activated sludge, the lack causing denitrification processes, and the final mixture is aerated, which keeps the activated sludge in suspension and in the course of the plug flow it leads to a gradual oxygen saturation and hereby to a gradual change from the denitrification to the nitrification with simultaneous purification of the added waste water, which causes the purification of the waste water before the said removal of the purified water by the fluidized bed filtration, while through the nitrification formed nitrates return with the activation mixture into the denitrification process and so in course of one circulation all processes of the complex waste water purification take place. Considering the effectiveness of the waste water purification it is a contribution that in the same time period the quantity of the purified water which is being taken away from circulation circuit through the fluidized bed filtration is smaller than the quantity of the activation mixture circulating in the circulation circuit. It is advantageous that the activation mixture mixed with the raw waste water is oxidized gradually through the aeration with a simultaneous suspendation of the activated sludge till the concentration of the dissolved oxygen in the activation mixture is at least two milligrams of oxygen per one liter of the activated mixture. Considering the control over the waste water purification process it is essential that the aeration is executed by a pneumatic aeration with a varying intensity as a function of the time and/or place in the circulation circuit. To reach a needed effect of the activation it is essential that the circulation intensity of the activation mixture is at least the double of the purified water throughput. Considering the bringing of the activation mixture in the plug flow it is a contribution that the activation mixture is brought into the circulation circuit by the raw waste water admission, by draining off the purified water and by forced admission of the activation mixture thickened by the separation into the circulation circuit behind the separation process. To increase the effectiveness of the denitrification it is significant that the purified water is taken away during each circulation by fluidized bed filtration from oxid part of the circulating activation mixture. The subject-matter of the apparatus according to the invention is that always two separation spaces are arranged adjacent to each other by their longitudinal sides, in which communicative connections with the activation space are formed and the longitudinal distribution channel 5, formed between the said longitudinal walls is completely closed by an end wall at one side, while at the opposite side a passage is arranged, by means of which it is connected with the flow channels system, the channels being laterally parted from the separation space, and the flow channel system and at least one distribution channel 5 form a part of the circulation circuit, another part of the circulation circuit being formed by a collecting equipment connected to the outlet for the activation mixture from the separation space, said collecting equipment being connected to at least one pumping set, the mouth of which forms the beginning of the circulation circuit, while the raw water admission mouths either into the admission area of the pumping set or into its mouth area, and the circulation circuit is provided with at least one baffle plate. To keep the sludge at a sufficient age and the circulation intensity in the circulation circuit it is advantageous that the collecting equipment is arranged near to the bottom of the separation space for fluidized bed filtration, the communicative connection with the activation space being formed by the upper opening and the lower opening, both of which are located at the same side of the separation space, the upper opening is connected with the extension of the separation space and the lower opening is near to its bottom, while the upper opening is smaller than the lower opening, so that it forms a resistance against the streaming of the activation mixture. Considering the hydraulic relations in the reactor and the simplicity of the construction of the separation space it is substantial that the separation space is connected with the activation space through a passage formed by a break in the partition of the separation space at the tank bottom, while a collecting main with inlets for thickened activation mixture is arranged in the separation space near to the tank bottom, the collecting main being connected with a pump, the outlet of which mouths in the activation space. Considering the construction and reconstruction of waste water purification plants it is essential the circulation circuit is formed by at least one basic module, in which the distribution channel 5 is formed by two inner partitions and the outer partitions form always together with the inner partition a separation space and together with the circumferential wall of the tank or with the outer wall of the next module a circumferential flow channel, while the distribution channel 5 is at its front connected with the circumferential flow channel and at its side with the separation space. Considering the effectiveness of the biological purification it is essential that the collecting sump, provided with a pump, is arranged in the circulation circuit, while outputs of the collecting equipment, bringing the activation mixture, mouth in said sump, and the the outlet from the pump mouths behind the baffle plate at the beginning of the flow channel, the raw water admission mouthing in the collecting sump. To provide a unified system for inner structure of reactors it is advantageous that additive modules of an identical embodiment are adjoined in the perpendicular direction to the basic module, eventually the basic module is arranged with its axis going through the center of the tank and the additive modules are arranged symmetrically and perpendicularly to the basic module. It is also an advantageous embodiment wherein at least one additive module is parallel adjoined to the basic module, the system of parallel modules formed in this way being symmetrical to the axis going through the center of the tank. To maintain a link-up of the separate processes of the waste water purification it is essential that the aeration elements are in the admission area for the raw waste water arranged with farther spacing than in the next parts of the circulation circuit, the cross sectional area of flow of the inlet opening into the fluidized bed filter being larger than 10% of the surface area in the separation space. An improvement of the denitrification course is reached by providing the collecting equipment with at least one pump, preferably centrifugal pump, which is arranged in the collecting sump. Considering the construction of big municipal waste water purification plants it is a contribution that the separation space for fluidized bed filtration is arranged through the whole length of the distribution channels of the circulation circuit, while the inlet of activation mixture into the separation space for fluidized bed filtration and the collecting equipment for carrying the thickened activation mixture out from the separation space are formed through its whole length. For the effective removal of floated sludge is good that a trap for flotated sludge is arranged in the upper part of the separation space, said trap being formed by a sloping roof, to the lower side of which a pressure air supply is adjoined, the upper part being provided with a flotated sludge outlet in the form of an air-lift pump mouthing in the activation space, while the whole roof is under the tank surface area. For preventing the influence of the flow in the distribution channel 5 onto the flow pattern in the separation space it is important that at least one flow deflector is arranged in the area of the passage to the partition from the side of the activation space. Considering the intensity of the nitrification it is advantageous that a mixer is arranged at the beginning of the activation space and the outlet from the pump mouths in the mixer, in which admission for raw waste water mouths and the outlet from the mixer mouths in the following part of the activation space. Due to the possibility of cleaning the collecting pipes it is important that the pump aggregate is a pump provided with a submersible reversible electric motor. For the possibility of taking off the electric motor and the runner of the pump aggregate it is advantageous that the reversible electric motor and the runner of the pump are arranged slidingly on guiding bars, located vertically to the tank bottom. Considering the keeping an optimal length of the collecting pipes it is important that the pump is connected with at least two branches of the collecting main. To enable an interrupted or controlled supply of the air it is important that the aeration hoses are located in the activation space and are connected with the pressure air supply through a closing or through a regulator. For better use of the air oxygen it is important that the aeration hoses are arranged in two branches which are located mutually at the opposite sides of the cross-section of the circumferential channel. The method and apparatus according to the invention represent a very effective means for prevention the eutrophisation in the water supplies in the nature. The main advantage is a high effectiveness of the purification for both removal of the the organic substances from the waste water and reducing the content of the eutrophisation elements, i.e. nitrogen and phosphorus. A complex waste water purification, especially municipal waste water purification is hereby provided by a simple method for activation purification without the necessity to add additional procedures for denitrification and dephosphatisatio . This significantly simplifies the technical solution of the reactors for a complex biological waste water purification. The module system of the reactor according to the invention allows a modular construction of the reactors in a wide range of capacity, up to the biggest reactors suitable for conurbations with millions of inhabitants. With channels formed by insertion the separation spaces for fluidized bed filtration into the activation space, the system of channels conection into a uniform circulation circuit allows a maximum simplifying and at the same time a shortening of the connecting ways between the linking up processes of the activation purification, including separation of the activated sludge with a minimum hydraulic resistance in the system. The system of activation mixture circulation allows also a spot inlet for raw water into the reactor, which lowers the cost of the raw waste water distribution in the waste water purification plant. Another advantage of the method and apparatus according to the invention is a high capacity resulting from a maximum use of the surface area of reactor for separation, allowing the reactor working with a high activated sludge concentration, which causes an increased qualitative and quantitative parameters of the apparatus. The method and apparatus according to the invention allow also a reconstruction of the hitherto existing classical waste water purification plants, which means an essential cost reduction compared with a construction of new waste water purification plants or an extension of old waste water purification plants. BRIEF DESCRIPTION OF THE DRAWINGS The invention will now be described in more detail with reference to exemplifying embodiments thereof, illustrated in the accompanying drawings, in which Figure 1 is a ground view at the basic module of the circulation circuit of the activation mixture; Figure 2 is a vertical section through the module along the line A-A in Fig.l; Figure 3 is a vertical section along the line B-B in Fig.l; Figure 4 a vertical section along the line C-C in Fig.l; Figure 5 is a axonometric view at the basic module of the circulation circuit according to Fig. 1 to 4; Figure 6 is a front view at the flotated sludge trap; Figure 7 is a sectional view along the line D-D in Fig.6; Figure 8 is a top view at the reactor with a rectangular ground plan resulting from adjoining other modules of the circulation circuit to the basic module of the circulation circuit; Figure 9 is a vertical section through the reactor along the line A-A in Fig.8; Figure 10 is a vertical section along the line B-B in Fig.8; Figure 11 is a vertical section along the line C-C in Fig.8; Figure 12 is an oblique view at another embodiment of the reactor with partial cuts; and Figure 13 is a schematical transversal crossection through the embodiment shown in Fig. 9. DETAILED DESCRIPTION OF EXAMPLES OF EMBODIMENT The apparatus according to the present invention comprises at least one circulation circuit. Each circulation circuit includes at least one basic module. In case the apparatus includes more modules or eventually one basic module and other additional modules, the embodiments of the basic module and the additional modules are preferably identical. In the • embodiment of the basic module of the circulation circuit according to Figs. 1 to 4 is the volume of a rectangular tank with the circumferential walls _!_, e.g. concrete walls, and with the bottom 8 . divided by a system of inserted partitions 2 . into functional spaces, i.e. spaces for both biological activation waste water purification processes and for flocculent suspension separation by a fluidized bed filter. In a preferred embodiment of the basic module, the adjacent inner partitions 2 . delimitate the separation spaces 4., which create the fluidized bed filter, each of them having a circumferential flow channel 1_ passing along one of its sides and a distribution channel 5_ along the other side, which ends up in the face 6 . , which completely closes the separation space 4 . for fluidized bed filtration and the distribution channel 5. There are two separation spaces 4_ abutting on each other by their longitudinal sides in the basic module, wherein the distribution channel 5_ is formed between them. Separation spaces 4 . spread essentially through the whole length of the basic module and communicate essentially through the whole length with the distribution channel 5_. The circumferential flow channels 1_ are located between the outer partitions 2 . and the circumferential walls 1 of the tank and they are separated from the separation spaces 4 . along their sides. The trap 29 . for flotated sludge and the collecting flumes 15_ for collecting the purified water are located in the upper part of the separation spaces 4 . for fluidized ' bed filtration. The separation space 4_ for fluidized bed filtration is completely closed by the face wall _______ at the opposite end, while the distribution channel 5 communicates with the circumferential flow channel 7 through the passage 6. The passage 2j5 has a rectangular shape, the longer side thereof being vertical (Fig. 3). This embodiment is easy to produce and is functionally satisfying. But the passage .26 may also have a different shape, e.g. the shape referring to the cross section of the distribution channel .5 in order to achieve a minimum hydraulic resistance. There may be also formed a not shown module comprising only one separation space 4 . . In that case the circumferential flow channel 1_ is formed along a longer side and a shorter side of the separation space 4 . while the distribution channel 5. is formed along the other longer side. By arranging two of these not shown modules side by side the above mentioned basic module with two separation spaces 4 . results. The flotated sludge trap £2 (Fig- 6-7) is immersed under the surface. It comprises a sloping roof with the head 40 (Fig. 7). The essential part of the roof is horizontal, while the head 4_p_ connected with the essential part or forming a single unit with it is inclined, its cross section thus gradually altering. The head 40 . is at a relatively small angle with the horizontal plane. The lower ending of the trap 22 is connected through the admission 38 . with a not shown separate pressure air supply with an overpressure corresponding to a comparatively small immersion depth, that means that the trap £2 is aerated. At the opposite - higher ending of the trap ^9 an outlet for flotated sludge is located, the main part of which is the air-lift pump 39, preferably connected with the same pressure air supply as the admission 3_8. The air-lift pump 32 may also be connected with another separate pressure air supply (not shown). The terminal of the air-lift pump 3_2 is led out at optional place at the flow channels Z, 9_. Sludge withdrawal may be continuous or intermittent, i.e. the pressure air supply, eventually pressure air supplies may be active permanently or intermittently essentially in dependence on the flotation rate. The present invention may be used also without the trap 22, e.g. in a case where no increased sludge flotation in the separation occurs. The partitions 2 . are angular in the upper part of the separation space 4. (Fig. 2,3,9,10). The lower part 1J2 of the separation space 4 . is linked to the upper part, the partitions 2 in the lower part 2=2 . being preferably straight and parallel to each other. There is the upper opening 10 formed in the upper part of each separation space 4 . and the lower opening ILL in the lower part 12 . . Both openings l_p_, ii_ form a communication connection from the distribution channel 5 . to the separation space 4 . and they are both at the same side of the separation space 4 . . The upper opening 10 is linked to the extension of the separation space 4 . and forms thus at the same time the inlet for activation mixture into the separation space 4_. Said upper opening 10 . is as a rule provided by a smaller inlet cross section than the lower opening Tl, the upper opening l__ causing a additional resistance for the activation mixture streaming from the distribution channel 5 into the separation space 4 . (Fig 2,3). The upper opening 10. forms preferably a slot spreading through the. whole length of the separation space 4 . , eventually an intermittent slot or separate, uniformly located slot openings. The axis of the lower parts l . of the separation spaces 4 . is preferably vertical, but it may be also oblique, so that the lower part 12 . of the separation space 4_ is deviated from the distribution channel 5_. The lower opening 11 . is arranged near to the bottom of the separation space 4 . , it is realized as openings in the wall of the lower part 12. of the separation space 4. and its total cross-section is larger than total cross-section of the upper opening 10 up to its multiple. The lower opening 1JL is intended particularly for drawing the activation mixture into the lower part 12. of the separation space 4 . , for equalizing the levels in the separation space 4 . and in the activation space and also for sludge removal when the operation is interrupted. The size of the inlet opening 14 . into the fluidized bed filter is in the big municipal waste water purification plants - with a low hydraulic unevenness factor up to 1.5 - at least 10% of the separation surface. The outlet for the thickened activation mixture from the separation is connected to at least one collecting equipment with at least one pumping set. According to a preferred embodiment the collecting mains 13 . of the collecting equipment are located near to the bottom of the lower parts 12:, the collecting mains being connected with collecting sump 3_5, wherein at least one pump, preferably a centrifugal pump 3_6», is located, and this pump is also a source of local turbulence. Outlet 2J_ of the pump 3_6 . is directed to the circumferential flow channel 1_ behind the baffle plate £1B as viewed in the direction of the activation mixture flow (Fig.l). Baffle plate 2B_ closes the head of the circumferential flow channel 1_, either completely, which is a preferred embodiment, or at least partly. It is essential that the outlet .27 together with the admission 2_2 for the raw sludge mouths in the circulation circuit in the flow direction behind the separation spaces 4_. So the raw water admission .22 . may mouth either in the inflow area of the pumping set or in the outlet area of the pumping set behind the baffle plate 28_. The raw water admission .22 . is preferably directed in the collecting sump 3_5_ (not shown in Fig. 1). The distribution channel 5_ communicates through the upper opening 10 . with the separation spaces 4 . and through the lower opening 1JL with the collecting main 1_3 . (Fig. 1,8), wherein at least one pump is included as a pumping set, e.g. an air-lift pump (not shown) or more air-lift pumps (not shown) , eventually the said centrifugal pump 36 located in the collecting sump 3_5 (Fig. 1,8,11), as mentioned above. If the centrifugal pump 3_6 located in the collecting sump 3_5 is put into practice, no air-lift pump is used, eventually the air-lift pump is included in some of the branches of the collecting main 13 . only in order to increase the mixing effect in the thickened activation mixture leaving the outlet 21_ and falling in the activation mixture in the tank, eventually into the collecting sump 35. The air-lift pump - or the centrifugal pump 3j5, if the collecting sump 3_5 is included - mouths with its outlet 27 into the circumferential flow channel 1_ behind the baffle plate 2 _ (Fig.l). The centrifugal pump 3> may also be replaced by the air-lift pump. Both kinds of pumps may be located either in the collecting sump 3_5 or outside the collecting sump 35, in every case the pump is a part of the outlet from the collecting sump 35 . , adjoining thus the collecting sump 35. Through this mutual connection between the circumferential flow channel 1_, distribution channel 5., separation spaces 4 . and by means of the collecting main 1_3 of the collecting equipment and the collecting sump 3_5 through back connection through outlet 22 with the circumferential flow channel 1_, a circulation circuit for the activation mixture is formed, wherein the activation mixture flows in a plug flow. The circumferential flow channel 1_ is over the whole length completely separated from the separation spaces 4 . by the partition 2 . . The aeration elements 3_ are placed near to the bottom in the circumferential flow channel 2 and in the distribution channel 5 . , preferably with various spacings so that different sections of the circulation circuit have different aeration intensity. According to the preferred embodiment the aeration elements 3_ are in the raw sludge admission area located so that they are spaced farther from each other than in the next parts of the circulation circuit. It is also possible to locate the aeration elements 3 . with equal spacings but with different aeration intensity at different places of the circulation circuit, the inventive apparatus may be thus adapted to different conditions. It is also possible to use aeration elements with a time variable aeration intensity. The above mentioned baffle plate JJ is located in the circumferential flow channel 1_ at the face wall side with the passage 2β_ into the distribution channel 5_. There is a raw water admission . 22 . leading behind the said plate 28 together with the outlet 22 of the air-lift pump or air-lift pumps (not shown) , eventually the centrifugal pump 36. The circumferential flow channel 2 has got in its longitudinal parts along the separation spaces 4 . a form of a narrow corridor, its cross section being formed by the shape of the separation space 4_. As a rule the circumferential flow channel 2 extends downwards first (Fig. 2) and in the lower part its walls are vertical and parallel. If using a different form of the separation space 4 . , the walls of the circumferential flow channel 1_ may be e.g. angular and parallel, eventually angular and divergent. The operation of the described basic module of the circulation circuit and the method for biological activation waste water purification with a dynamic nitrification and denitrification is as follows: The activation mixture circulates in the circulation circuit by a plug flow and it is continuously oxidized by a pneumatic aeration, which at the same time secures a suspendation of the activated sludge. So all individual particles of the activation mixture advance in the circulation circuit with at least one vector component of its speed in the direction of the activation mixture flow as a whole in the circulation circuit. It is thus advantageous that through the operation of the aeration elements 3_ the individual particles move also in the level perpendicular to the advance in the circulation circuit and perform e.g. a helicoid movement. To reach a high activated sludge concentration in the circulation circuit, the activation mixture is object of fluidized bed filtration in course of every circulation, during which the purified water is separated from the mixture, while the separation is performed in the separation spaces 4 . , which cover practically the whole surface of the tank with the circumferential walls 1. Purified water separated through fluidized bed filtration is taken away by collecting flumes 15 and its quantity is always lesser than quantity of the activation mixture circulating in the circulation circuit during the same time period. It is advantageous that the purified water is taken away by the luidized bed filtration from a part of the circulating activation mixture only, what enables to reach a high circulation intensity and herewith high denitrification degree is possible. This is achieved according to the exemplifying embodiment by drawing the activation mixture from the distribution channel 5 through the lower opening 11 . in the collecting equipment area near to the bottom of the separation space 4 . . The circulation is performed by raw waste water admission, by pumping the thickened activation mixture from the fluidized bed filter back into the circulation circuit behind the baffle plate .28 . and by purified water outlet through the collecting flumes 15 . . The activation mixture is herewith brought in the circulation circuit with a plug flow character. Raw waste water is admixed into the circulation circuit, preferably behind the baffle plate .28 . or in the collecting sump 3_5. That causes an oxygen lack at the surface of the particles of the activated sludge, and it starts denitrification processes. The activation mixture is then by effects of the aeration elements 3 . gradually oxidized by aeration with simultaneous suspendation of the activated sludge during the circulation in the flow channels 2 till the conditions necessary for nitrification processes are reached, and then the activation mixture is subjected to a fluidized bed filtration in the separation spaces 4 . . Raw waste water is admixed into the thickened activation mixture with nitrate originated through the oxidation of the nitrogen pollution, e.g. in the collecting sump 3_5, and herewith all processes of the complex waste water purification with organic and nitrogen substances removal are realized during one circulation. As a rule the activation mixture is gradually oxidized through the aeration till the concentration of the oxygen dissolved in the activation mixture reaches or exceeds at least two milligrams of oxygen per one liter of the activation mixture. Herewith an optimum process of biological waste water purification is realized, as it will now be below described in more detail. The activation mixture enters the separation spaces 4_ for fluidized bed filtration through the upper opening 10 and the extending space of the separation space 4 . , and it is brought through the inlet opening _1 from the lower part 12 . into the extending part of the separation space 4_, wherein the fluidized bed filtration is realized. The effectiveness of the separation through the fluidized bed filtration depends among others on the size of the inlet opening 14. The optimum size of the inlet opening 14 . is at least 10% of the separation surface in big municipal waste water purification plants with a low hydraulic unevenness coefficient up to 1.5. The separation of purified water from the activated sludge is performed in the fluidized bed filter in the separation space 4_ by fluidized bed filtration, wherein the water deprived of the activated sludge suspension is led away through collecting fumes 15 from the purification system. The flotated sludge intercepted on the trap 29 ^ is brought into the activation space, as a rule at an arbitrary place in one of the flow channels Z. ϋ- Through filtration thickened activated sludge sinks countercurrent-wiεe through the inlet opening 14 . into the lower part 12 . to the collecting main 13 arranged near to the bottom of the lower part 12 . . The outlet 21_ of the collecting equipment, eventually in absence of a pump, the collecting main(ε) 13 . itself mouths in the collecting sump 35, wherefrom the activation mixture is pumped off by a centrifugal pump 36 . , this pump causing a strong local turbulence. The local turbulence excited by the centrifugal pump 36 is necessary to release gaseous nitrogen bubbles which stuck at the particles of the activated sludge during the denitrification process. The flowing of the activation mixture in the collecting sump 35 is of a gravitational type owing to a difference between the level in the tank and in the collecting sump 3J5. If the local conditions call for it, it is also possible to place a pump in the collecting equipment, e.g. an air-lift pump. The lower opening 3JL allows also in case of an interruption in the reactor aeration a pasεage of the activated sludge from the separation space 4 . into the distribution channel 5 . , and herewith an undesirable silting with sludge in the lower part 12. is prevented. The lower opening 11 . secures at the same time a level equalizing in separation and activation during the filling of the reactor or during the sludge blow-off, and this allows a pressurelesε solution of inner structure of reactor. Raw waste water is admixed in the circulation circuit in the circumferential flow channel 2 into the activation mixture thickened after the fluidized bed filtration, said waste water causing a shock drop of the dissolved oxygen concentration in the activation mixture especially at the surface of the particles of the activated sludge, and herewith it provides good conditions for dynamic denitrification. The denitrification processes nevertheless don't require anoxid conditions in the whole volume of the activation mixture, form ation of local anoxid conditions at the surface, eventually at the surface of the activated sludge particles is entirely sufficient. The shape of the circumferential flow channel in the form of a narrow corridor makes it possible that also a little aeration intensity is sufficient for a suspendation of the activated sludge during a considerable flowing speed of the activation mixture. The denitrification regime needing a low oxygen content in the activation mixture is not impaired by that. At the running aeration during the plug flow it comes to a biodegradation of the polluting substances in the activation mixture through oxidation and a gradual saturation of the activation mixture with oxygen up to the reaching of conditions for nitrogen substances nitrification, what is usually achieved through a value over 2 mg 0 /1. An increased content of the disεolved oacygen iε favourably shown also in the effectiveness of the following activated sludge separation through the fluidized bed filtration, because a higher oxygen content in the activation mixture prevents denitrification processes during the fluidized bed filtration. It prevents the flotation of the activated sludge in the separation space 4 . and also the releasing of the phosphorus into the purified water. The circulating activation mixture brings nitrates, originated in the nitrification zone with sufficient oxygen content, into the circulation circuit zone with a lowered disεolved oxygen content. Then the nitrates are reduced to a gaseous nitrogen in said zone with a lowered oxygen content, and so the denitrification iε performed. Bubbles of the gaseouε nitrogen which stick at the activated sludge particles during the denitrification are removed with the circulation of the activation mixture in the circulation circuit by a movement supply with a high local turbulence intensity, e.g. by a centrifugal pump ,36 . . The εtreaming power for calling intensive local turbulences may be advantageously used for admixing the circulating activation mixture with the purified waste water, wherein the raw waste water admixed into the circulating activation mixture causes besides a lowering the content of dissolved oxygen, also carbon supply necessary for denitrification procesεeε. The effectiveness of the described dynamic waste water denitrification in the circulation cycle of the activation mixture with periodical alternation of the nitrification and denitrification process depends on the circulation intensity of the activation mixture according to the expression 1 T [%] = 100, n + 1 wherein T iε the effectiveneεε of the denitrification given in percentε n iε the proportion of the water quantity running through one croεs section in the circulation circuit in a time unit to the raw water quantity being brought in the same time unit. This proportion repreεents a circulation intensity in the circulation circuit. E.g. to reach a 75% effectiveness of the nitrates reduction according to the above mentioned expression a triple circulation intensity compared with the purified raw water quantity iε necessary. Described process of biological waste water purification is usually effective with an intensity of the activation mixture circulation being within the range of double up to sextuple of the purified water quantity. The circulation intensity may be also much higher for very concentrated waste water and therefore the quantity of the water running through the circulation circuit may be a multiple of the raw waste water being brought. Then it is alεo necessary that the sucking of the activation mixture through lower opening to the collecting equipment inlet is higher. That iε given by the dropping reεiεtance value, i.e. by the εize of the upper opening 10. The total intenεity of the biological purification processes depends on the concentration of the activated sludge in the purification system, which is directly dependent on the separation intenεity. The circulation of the activation mixture in the circulation circuit neceεεary to reach the required denitrification intenεity increaεeε the claims for separation capacity. An integral insertion of the fluidized bed filtration in the circulation circuit of the activation mixture, with a full use of the whole activation surface for separation, secures a high concentration of the activated sludge, which secures then a low sludge loading necesεary for the nitrification aε the main objective for nitrogen pollution removal from waεte water. An important quality of the deεcribed method of dynamic nitrification and denitrification iε also its high effectiveness of phosphates removal from waεte water, that with a total reduction of phosphorus up to 80%. According • to the described method all processes of complex biological purification with a removal of organic and nitrogen subεtanceε and alεo with a high effectiveneεε of phoεphates removal from waste water are accomplished in one circulation in the circulation circuit. Example of the method No. 1 The described method according to the invention performed in a communal waste water purification plant of a mountains recreation center, and before all documentation of results of this method is in question. For the waste water purification plant a seasonal load is characteristic with maximum values in winter and summer. The top hydraulic load is 200 3 in an hour and in a period out of season it is 100 3 . Such a plant has also remarkable deviations of the substance load with maximum values in summer and winter. The average concentration of the pollution in season or out of season shows the following table I. TABLE I where BOD iε biological oxygen demand in five dayε per one kilogramme of volatile suspended solids of the activated sludge COD is chemical oxygen demand SS εuεpended εolids P tot total amount of phosphorus in the waste water N org amount of the organic bound nitrogen N tot total amount of nitrogen Example of the method No. 2 The described method of the biological purification used for pig manure purification is in question. The pig sewage presents an example of extraordinarily polluted waste water having a concentration of organic substances, nitrogen and phosphorus, which exceeds the concentration of the communal waεte waterε in the order. Again the documentation of the results of the method according to the invention iε in order. The input values of the pig manure after a mechanical separation of the rough components εhow the table II. TABLE II A controlled εystem of aeration was used, namely gradually different intensity of the aeration in the circulation circle with the controlled time course of the aeration according to the invention. At the outlet following parameters of water mentioned in table III were achieved. TABLE III amount in mg/1 COD 160 BOD ^ 20 SS 5 N-NH "* 20 N tot 30 P tot 3 The embodiment according to Fig. 8 to 11 iε a modular one, based on the basic module of the circulation circuit. An increase of the reactor capacity is obtained by adding other modules of the circulation circuit to the basic module. The number of adjoint modules may vary and so it is poεεible to form a reactor in a modular way with a capacity responding to a need. A preferred solution is formed by a multi-unit arrangement of several adjoint modules without another partition between them, aε shown in crosε εection in Figs. 9,10. In that exemplifying embodiment right-angled tank having circumferential walls 1 is divided by a system of inserted partitionε 2 . into functional spaces for activation biological processes of waste water purification and for separation of flocculent εuεpenεion by a fluidized bed filter in the same way as in the basic module in the circulation circuit. What is different is that the separation spaces 4 . divide the activation space in distribution channels 5_ and new inlet flow channels 9 . , wherein the distribution channels 5 are the same as in the single basic module, while the inlet flow channel 9 . is not present in the εingle basic module and it is formed esεentially by two opposing circumferential flow channels 7 of the basic module. The distribution channels 5_ and the inlet flow channels 9_ are closed at one end by faces 6 . , which entirely close the separation spaces 4 . and the distribution channels 5_. Nevertheless, the faces <5 are interrupted at the end of the inlet flow channels 9_, forming pasεages 2J5, by means of which the inlet flow channels 9 are connected with the circumferential flow channel 2 (Fig * 8). The passages 25_ have got the same form as the paεsages of the baεic module. The flow channelε, e.g. the circumferential flow channel 1_ and the inlet flow channel 9 . , are in all embodiments at their longitudinal sides entirely separated from the adjoining spaces, especially from the separation spaces 4 . . The flow channels are designated as inlet flow channel 9_ and circumferential flow channel 2 just to make the arrangement clear, because the circumferential channel l_ iε arranged along the circumferential wall 1 . of the tank and the activation mixture enterε the inlet channel £ before it enterε the distribution channel 5 . . But the designation "flow" is more esεential for both of εaid channelε becauεe both are intended for plug flow of the activation mixture, without permiεεion the activation mixture to get away from these flow channels 1_, 9_ and also without changing the flow volume in these serially connected channels. The separation spaces 4 . and the inlet flow channels 9_ are at the other end quite closed by the face walls 6 ' . These face walls 6J are also interrupted and thus at the places of the interruption form the paεεages ^6 in a similar way as in the above mentioned baεic module, wherein the diεtribution channels 5_ communicates through the pasεages 26 with the circumferential flow channel l_. The separation spaces 4_ for fluidized bed filtration are connected with the distribution channels 5_ in the εame way aε in the baεic module. There are no circumferential walls between the adjoint moduleε of the circulation circuit - in the exemplifying embodiment of the reactor there are three modules - so that by adding two moduleε to each other the flow channel 9 . ariεes, as mentioned above. The module in the embodiment according to Figs. 8 to 11 perpendicular to the adjoint moduleε is modified. Unlike the individual basic module according to Figs, l to 5 this modified basic module has no passage .26 . formed in the face wall 6_ , so that the diεtribution channelε 5 are cloεed at both εideε. So the diεtribution channel 5_ of thiε modified baεic module (Fig.8) doeε not communicate with the circumferential flow channel 7 of the modified basic module. In addition the separation spaces 4 . are divided into two parts, a collecting sump 3_5 being arranged between them. There are two baffle plates . 28 used therefor (Fig.8). The modified basic module is separated from the adjoint modules system by a partition wall 3__, wherein passages 41 indicated by arrows in Fig.8 are formed. The pasεage 4_l connects always the circumferential channel 1_ of the modified basic module with the beginnings of the inlet flow channelε 9_ of the adjoint modules. The circumferential flow channel 1_ of the adjoint modules is connected through the interconnection 3_0, for example through pipes, with the distribution channels . 5 of the modified basic module (Fig. 8) . The outlets TJ- °f the collecting mains 1_3_ mouth in the collecting sump 3_5. It iε alεo within the scope of present invention to form another modifications of connections between the adjoint modules and perpendicular modified basic module. The function of the reactor according to Fig. 8 to 11 is essentially identical with the function of the basic module in the circulation circuit described above. Raw waste water iε brought into the collecting εump 3_5, wherefrom the waεte water, mixed with thickened activation mixture, iε diεcharged into the area between collecting εump 3_5 and the partition wall 34.. It flowε further towards the circumferential flow channel 1_ of the modified basic module - in Fig. 8 below. It flowε then in both εideε through the circumferential flow channel 2 as far aε to the partition wall 3_4 and through the paεεageε 4JL in said partition wall into the inlet flow channelε 9_ of the adjoint modules (Fig. 8) , wherefrom it comes into the circumferential flow channel - as shown in Fig.8 above. The activation mixture flows out of it further through the circumferential flow channels 2 along both sides of the tank. It advances further through the circumferential flow channel 2 along the modified baεic module and enters the distribution channels 5_ of the adjoint modules through the paεεageε 2j5 and alεo the diεtribution channelε 5_ of the basic module through the interconnection 30 - formed for example by pipes. The activation mixture comes from the distribution channels 5 . into the separation spaces 4 . , as mentioned above. The thickened activation mixture from the separation spaces 4 . iε brought by the collecting equipment, eεpecially by the collecting main 13 and outletε 22, into the collecting εump 35. Another alternative of the apparatus according to the present invention (not shown) has got a circular tank, wherein the flow channels 9., Z, "the distribution channels 5_ and the separation εpaces 4 . are arranged similar to the embodiment shown in Fig.8 with the difference that the length of the separation spaces 4 . and the shape of the circumferential flow channels 2 are adapted to the tank shape. Said embodiment iε suitable mostly for reconstructions of circular sedimentation basins common e.g. in already existing and used municipal waεte water purification plants of the clasεical type, to increase their quality and quantity parameters. Through reconstruction of the circular sedimentation basinε in the hitherto existing municipal waste water purification plants it is posεible to keep the original raking bridge (not shown) and to use it to access the individual places of the reactor tank doing the operational control. The function of the reactor is at the same time essentially identical with the function of the preceding exemplifying reactors described above, especially with that of the reactor according to Fig. 8 to 11. Another variant of the apparatus according to the invention iε shown in Fig.12 and 13. In the rectangular tank with the circumferential wall 1 are through inserted partitions 2_ and face walls 6 . and 6J created two longitudinal separation spaces 4., spreading out in the upwards direction. The partitions 2 . are advantageouεly in their lower parts connected to the bottom of the tank and with their upper parts to a not shown carrier construction. Separation spaceε 4 . create in the tank between the partitionε 2 . and face wallε § . ,§_' the diεtributing channel 5 . , which iε a part of the activation space. The face wall of the εeparation space 4_ reacheε up to the circumferential wall 1 and createε thuε the partition wall 2S_, which similarly to the previous alternative separates the circumferential flow channel 2- The other face wall 6J closes not only separation spaceε 4., but it separateε alεo the distribution channel 5_ from the circumferential flow channel 2- The circumferential flow channel 7 is a through flow channel, it does not communicate with any other space except of distributing channel 5 . , which is linked to it. In the oppoεite face wall 6 . an inlet .24 . to the diεtribution channel 5 . iε created. The εeparation space 4 . is along to its complete length connected with the distribution channel 5_ and due to it also with the activation εpace through the only one paεsage 1 , which is arranged in at least one breaking of the partition 2 . at the bottom of the tank (Fig.13). The passage 1 can be either along its length without break or it can be made as a set of orifices in the partition .2 of the separation space 4_. Partitions 2_ have in the cross section advantageously an arc form (Fig.2) . The partitions 2_ expand from each other in the upwards direction and they thus create the prismatic separation space 4 . for the fluidized bed filter. The partitions 2 . are at the same time at the bottom separated from each other and between them is at the bottom arranged the perforated collecting piping 13 . , which is mouthed to the pumping aggregate 25_. The partition 2 . can be made from a smooth material or from a profiled material. It is advantageous to make the profilation in the direction from above to bottom, what ensueε in forming of low ribε on the surface of the partitionε 2. In the area of the passage 19 ^ at least one flow rectifier . 20 . is added to the partitions 2_ from the side of activation space, i.e. from the side of distribution channel 5 . . It is determined for the separation of the flow of activation mixture in the diεtribution channel 5_ from the flow in εeparation space 4. The flow rectifier 20_ iε advantageously attached to the partition 2 . and it iε orientated vertically and it iε extending εubstantially along the full length of partition 2_^_ It is posεible to arrange along the length of partition 2_ a number of flow rectifierε 2O_ linking to each other. The flow rectifier 2Q_ iε arranged at the lower part of the partition 2 . , itε lower edge being situated over the lower edge of partition 2 . , but it reaches at most to the level of edge of the partition 2 . It iε nevertheless also posεible to leave this flow rectifier .20 . out. When the flow rectifier 20 . is applied, it restricts the transfer of turbulenz from the activation space to the separation space. Itε efficiency can be higher at the profiled partitionε 2 . or even at smooth εeparation walls, where the profilation is made only in the area of attachment of flow rectifier ,20 . , where it iε attached to the ribε of profile of partition 2 . and thuε does not abut tightly to the separation wall in the whole area of joint. In this way a small part of activation mixture between the flow rectifier .20 . and partition 2 comes to the area of passage 1_ and it supports the restriction of transfer of turbulenz from the distribution channel 5 . of the activation space. The pumping aggregate 4JL consists of the pump body, in which the collecting piping 13 . iε mouthed and which iε attached to the bottom of the tank, and from a moving pump wheel which is connected through the shaft to an immersion electric motor, which is advantageously a reverεible one. Rotating parts of the pumping aggregate 4JL are mounted with the possibility of drawing them out above the level of the reactor during its operation. Into the pumping aggregate 4TL the collecting piping from the other separation εpace 4 . is mouthed, pumping aggregate 4JL being thuε common. In caεe of great length of the εeparation εpaceε 4 . the pumping aggregate can be advantageouεly placed in the middle of the length of the diεtribution channel 5. In that caεe are to the pumping aggregate from the both neighboured εeparation εpaceε 4 . mouthed four collecting pipings 33 . , alwayε two and two from each εide. At the great length of the reactor it iε poεεible to arrange a number of pumping aggregateε behind each other in order to reduce the length of the collecting piping 3-3 . to 12 meterε, what iε the optimum length for the collecting εyεtem. Power unit of the pumping aggregate ,41 . iε the electric motor 42 . . On the not εhown carrier conεtruction an elevating mechaniεm (not εhown) is placed. Reversible electric motor 42 and moving wheel of the pumping aggregate 4_1_ are mounted εlidingly on the guide εtabε, which are arranged perpendicularly to the bottom of the tank. Due to this elevating mechanism it iε poεεible to pull out the εubmerged reversible electric motor 4_2_ and the moving wheel of the pumping aggregate 41 . on these (not shown) guide stabε even without the emptying of the tank. Pumping aggregate 4_1 and itε power unit are modified for the reverεible moving for the reverεe flow of the activation mixture in the collecting piping 13. At the beginning of the diεtributing channel 5 . and thuε at the beginning of the activation space a mixer 4j5 for the mixing of activation mixture with the raw waεte water iε arranged. The outlet 4 . 3 from the pumping aggregate 4_1 iε brought behind the partition wall ,28 . at the beginning of the circumferential channel 2 "to the mixer .46 . , into which also the inlet .2J2 of the raw waste water is mouthed. Mutual interconnection among the circumferential channel Z - distributing channel 5., separation space 4. and the collecting syεtem, created by the collecting piping 13 and pumping aggregate 4_1, formε an inner circulation circuit. From the above deεcribed reεultε that the collecting piping 13 . could be εpecified alεo aε a recirculation piping, becauεe through it the activation mixture comeε back to the circulation circuit. The circumferential channel 2 and the diεtributing channel 5 . are equipped with an aeration system consiεting of the row of perforated elaεtic aeration hoεeε 42, connected to a common diεtribution εyεtem 44 . of the pressed air. The (not shown) orifices in the perforated elastic aeration hoseε 42 are advantageouεly εmall for the creation of εmooth bubbleε by the aeration. Every aeration hoεe £7 iε equipped, with an independent valve 4_5 or with a (not shown) regulator for the regulation of the aeration intensity. Through location of various numbers of the aeration hoseε 42 in different places of the circumferential channel 4 . and the diεtributing channel 5_, the aeration intenεity according to the needε of purification process can be influenced. Another regulation of the aeration intensity in dependence on the time can be achieved by installation of a (not shown) blower with a changeable speed of rotation or by installing of bigger number of blowers and by starting them according to the needs of aeration. At an advantageous arrangement of the aeration hoses 42 in the activation space the aeration hoseε 47 are located in two brancheε, each of them can contain several aeration hoseε 42• These branches are arrangeε mutually at the opposite sideε of the cross-section of the circumferential channel 2, regularly near at the bottom of the tank. The upper part of the separation space 4 . is equipped by the overflow channels 1_5 . for the removal of cleared water after fluidized bed filtration. The described alternative according to the Figs.12 and 13 workε analogically with the previouε alternatives. The subject is an integrated reactor for biological waste water purification, wherein separation spaces 4_ for the separation of suspension of the activated sludge by fluidized bed filtration are built-in in the activation space. By building-in of εeparation spaces . 4 a syεtem of channelε iε created, said channelε being interconnected serially behind each other by the above described manner. The raw waste water is brought through the inlet piping to the mixer 4j6 at the beginning of the circumferential channel 2 in the direction of the flow behind the partition wall 2J3, where the pumping aggregate l_ alεo bringε the recirculated activation mixture from the εeparation spaceε 4 . by. In the mixer 46 . the raw waste water is perfectly mixed with the recirculated activation mixture. The bringing-in of the organic substances present in the raw waste water to the activation mixture induces an intermittent decline of the content of the dissolved oxygen, whereby at the beginning of circumferential channel 2 anoxid conditions for the denitrification processes are created. Suspendation of the activated sludge is in this anoxid part of the activation kept by the aeration with a very low intensity, which is satisfactory for keeping suspenεion in εuspendation, but anoxid conditionε for a proceεε of denitrification are not disturbed. Because of thiε the number aeration hoseε 47 in thiε part of the circumferential channel 2 is reduced. For improving of the suspendation it iε poεεible to equip thiε part of the circumferential channel 2 toy a not shown mechanical source of mixing, which eventually enables complete leaving out of aeration from this part of activation. The course of the denitrification procesε is checked by meaεuring of parameters of the activation mixture by using of probes (not shown), which bring the impulseε to the power unitε of the blowers. In such a way their speed of rotation and amount of supplied air is being changed. By the reduced intensity of aeration is the denitrification zone in the circumferential channel 4 . εpread out, whereby the intensity of denitrification arises. This procesε can be fully automated. During a plug flow of the activation mixture through the circumferential channel 2 the content of diεεolved oxygen iε gradually enhanced, thiε proceεε being a consequence of the enhanced intenεity of aeration and of the decline of content of biodegradationable substances.In such a way an oxide milieu for the aerobe activation processeε of the biodegradation of organic εubεtanceε and for nitrification of ammoniacal and organic nitrogen iε created. If the aeration hoseε 42 are arranged in two brancheε located at the oppoεite εideε of the cross-εection of the circumferential channel 2, it iε poεεible by meanε of the valves 45 . or not shown regulators to bring the air alternatively into one branch and then into the other branch. During bringing the air for example into the left branch a transverse circulating movement of the activation mixture originates. At interrupting the bringing of the air into the left branch and bringing the air into the right branch a counter-flow of the air and the activation mixture originates. The activation mixture due to the inertia continueε itε hitherto exiεting tranεverεe circulating movement up to the moment, when itε movement by action of the flowing air iε stopped and it begins to turn into the opposite senεe. Theεe operating cycleε may be regularly repeated by meanε of the regulation. Thus the time of the keeping of the air in the activation mixture iε extended, by which the oxygen transition into the activation mixture is increaεed. Another effect of the counter-flow of the air and the activation mixture is more effective suspendation of the activated sludge. In the distribution channel 5_ before the intake to the separation space 4 . the intensity of aeration can be arranged so that the content of disεolved oxygen coming to the layer of the fluidized bed filter in the εeparation εpace 4 . fully ensures oxyd conditions in the course of the whole separation procesε. A εhort time of the activation mixture in the separation space during the fluidized bed filtration, what iε the consequence of the small volume in which the separation take place, contributes to the optimum oxide conditions during the separation by the fluidized bed filtration as well. It is a result of the prismatic form of the separation εpace 4 . and of the high filtration εpeed in the fluidized bed filter. The deεcribed courεe of the activation biological waεte water purification with the changing of the oxide and anoxide conditionε in the circulation circuit cauεeε the accumulation of phosphoruε from the waεte water in activated εludge. During the following separation of the excesε activated εludge in the εeparation space the εtrict oxide conditionε preventε the reverεe releaεe of the accumulated phoεphoruε back to the purified water. In εuch a way a high efficiency of the biological purification proceεε, even where the removal of the phosphorus from the waste water is concerned, could be achieved. The clear water is taken away after its paεεage through the fluidized bed filter to the removal channelε 15. Aε it waε described, the separation εpace 4 . iε connected to the diεtributing channel 5 only through one paεεage 19 . , at which one or more rectifier(ε) .20 . of the flow iε (are) arranged. Thiε εimple εolution of the inlet of the activation mixture to the separation εpace 4 . iε enabled by an intenεive recirculation of the activation mixture in the circulation circuit with itε removal at the bottom of the separation space 4 . by the collecting piping 1_3. The intensity of circulation of activation mixture in the circulating circuit influences at the same time the efficiency of denitrification procesεeε according to the formula mentioned in the firεt alternative. From the bottom of the separation space 4 . the activated εludge separated in the εeparation space 4_ during the procesε of filtration in the fluidized bed iε sucked off, and together with the circulating activation mixture from the activation diεtributing channel 5 . , i.e. from the activation proceεε. The intenεity of the flow in the lower part of the εeparation εpace 4 . in conεequence of the recirculation of the activation mixture preventε a tranεfer of perturbationε from the aerated diεtributing channel 5_ to the εeparation εpace 4_. By this means the εtability of the fluidized bed filter in the εeparation εpace 4 . and a high separation efficiency are εecured. The restriction of the interconnection between the activation εpace and the separation space to an only pasεage 19 at the bottom of the tank εignificantly εimplifieε the conεtruction of the εeparation εpace 4 . . It enableε to use selfcarrying shell structure for construction of the separation space 4., which consiεtε of only two elementε, namely two εeparation walls * Theεe wallε are attached directly at the bottom of the tank and with itε other upper end to a not εhown εupporting εtructure. The εyεtem of connecting of more collecting pipingε 1_3 to one pumping aggregate 4L, eventually the inεtallation of more pumping aggregateε 41_ enableε keeping of the optimum length of the collecting piping 1_3 for big capacitieε of the waεte water purification plantε aε well, the length of the εeparation εpace of which could reach up to εeveral hundredε of meterε. The reverεible course of the pumping aggregate iε uεed to the purify the collecting piping by a reverse εtream of water. INDUSTRIAL APPLICABILITY The method and apparatus according to the present invention is εuitable both for new waεte water purification plantε conεtruction and for reconεtruction of hitherto exiεting claεεical waεte water purification plantε with individual activation and εedimentation tankε, especially for big capacity plants. Present invention may consequently be used for a relatively simple reconstruction of said existing waste water purification plantε reaching herewith a considerable intenεification, namely through increaεing their capacity and their purification efficiency, including phosphorus and nitrogen removal. List of partε : 1 circumferential wall 2 partition 3 aeration elementε 4 εepaiation εpace 5 distribution channel 5 6 faces 6' face wall 7 circumferential flow channel 8 bottom 9 inlet flow channel 10 upper opening : : : 11 lower opening : : : 12 lower part of the εeparation space 13 collecting mainε of the collecting mechanism 14 inlet opening 15 collecting flumeε 22 raw water admission 25 passage 26 pasεage 27 outlet 28 baffle plate 29 trap 30 interconnection 34 partition wall 35 collecting sump - drain sump 36 centrifugal pump 38 admission 39 air-lift pump 40 head 41 passage 42 electric motor 43 outlet 44 distribution system 45 valve 46 mixer 47 aeration hoseε

Claims: CLAIMS 1. Method for biological activation waste water purification, wherein the waste water is biologically purified by an activation procesε, during which a nitrification occurs, characterized in that the activation mixture is brought into the circulation circuit with a plug flow character, wherefrom the purified water is taken away by a fluidized bed filtration and the activation mixture is afterwards mixed with raw waste water, which causes an oxygen lack at the surface of the particles of the activated sludge, the lack causing denitrification processes, and the final mixture iε aerated, which keepε the activated εludge in suspenεion and in the course of the plug flow it leads to a gradual oxygen saturation and hereby to a gradual change from the denitrification to the nitrification with simultaneous purification of the added waste water, which causeε the purification of the waste water before the said removal of the purified water by the fluidized bed filtration, while through the nitrification formed nitrateε return with the activation mixture into the denitrification proceεε and εo in courεe of one circulation all proceεεeε of the complex waεte water purification take place. 2. Method aε claimed in Claim 1, characterized in that in the same time period the quantity of the purified water which is being taken away from circulation circuit through the fluidized bed filtration is smaller than the quantity of the activation mixture circulating in the circulation circuit. 3. Method as claimed in Claim 1, characterized in that the activation mixture mixed with the raw waεte water iε oxidized gradually through the aeration with a εimultaneouε suεpendation of the activated εludge till the concentration of the dissolved oxygen in the activation mixture is at least two milligrams of oxygen per one liter of the activation mixture. 4. Method as claimed in Claim 1, characterized in that the aeration is executed by a pneumatic aeration with a varying intensity as a function of the time and/or place in the circulation circuit. 5. Method as claimed in Claim 1, characterized in that the circulation intenεity of the activation mixture iε at leaεt the double of the purified water throughput. 6. Method aε claimed in Claim 1, characterized in that the activation mixture is brought into the circulation circuit by the raw waste water admisεion, by draining off the purified water and by forced admission of the activation mixture thickened by the separation into the circulation circuit behind the separation procesε. 7. Method as claimed in Claim 1, characterized in that the purified water is taken away during each circulation by fluidized bed filtration from a part of the circulating activation mixture. 8. Apparatus for performing the method as claimed in Claim 1, which compriseε in a common tank an activation space and upwards extending longitudinal separation εpaceε, from which the outletε for purified water are led out, and each separation space is defined by the partitions and the faceε and it communicates with the activation space at one longitudinal side, where between the partitions of the separation spaces mutually and between the partitions and the tank walls separated longitudinal channels are formed, in which the aeration elementε are arranged, characterized in that alwayε two separation spaces (4) are arranged adjacent to each other by their longitudinal sides, in which communicative connectionε with the activation εpace are formed and the longitudinal distribution channel (5) , formed between the said longitudinal walls is completely cloεed by an end wall at one εide, while at the opposite side a pasεage iε arranged, by means of which it is connected with the flow channels (9,7) syεtem, the channelε (9,7) being laterally parted from the separation space (4) , and the flow channel (9,7) syεtem and at least one diεtribution channel (5) form a part of the circulation circuit, another part of the circulation circuit being formed by a collecting, equipment connected to the outlet for the activation mixture from the separation space (4), said collecting equipment being connected to at least one pumping set, the mouth of which forms the beginning of the circulation circuit, while the raw water admission mouths either into the admiεεion area of the pumping set or into itε mouth area, and the circulation circuit iε provided with at least one baffle plate (28). 9. Apparatuε aε claimed in Claim 8, characterized in that the collecting equipment iε arranged near to the bottom of the separation space (4) for fluidized bed filtration, the communicative connection with the activation εpace being formed by the upper opening (10) and the lower opening (11), both of which are located at the same side of the separation space (4), the upper opening (10) iε connected with the extenεion of the separation space (4) and the lower opening (11) is near to its bottom, while the upper opening (10) is smaller than the lower opening (11) , so that it forms a dropping resistance against the activation mixture streaming. 10. Apparatus as claimed in Claim 8, characterized in that the separation space (4) iε connected with the activation space through a passage (19) formed by a break in the partition (2) of the separation space (4) near to the tank bottom, while a collecting main (13) with inlets for thickened activation mixture is arranged in the separation space (4) near to the tank bottom, the collecting main (13) being connected with a pump (41), the outlet of which mouths in the activation space. 11. Apparatus as claimed in Claim 8, characterized in that the circulation circuit is formed by at least one basic module, in which the distribution channel (5) is formed by two inner partitions (2) and the outer partitions (2) form alwayε together with the inner partition (2) a εeparation space (4) and together with the circumferential wall (1) of the tank or with the outer wall of the next module a circumferential flow channel (7) , while the diεtribution channel (5) iε at itε front connected with the circumferential flow channel (7) and at itε εide with the separation space (4) . 12. Apparatuε aε claimed in Claim 11, characterized in that the collecting sump (35), provided with a pump (36), iε arranged in the circulation circuit, while outletε (27) of the collecting equipment, bringing the activation mixture, mouth in said sump (35), and the the outlet (27') from the pump (36) mouths behind the baffle plate (28) at the beginning of the flow channel (7). 13. Apparatus aε claimed in Claim 12, characterized in that the raw water admiεεion (22) mouthε in the collecting εump (35). 14. Apparatus as claimed in Claim 11, characterized in that additive modules of an identical embodiment are adjoined in the perpendicular direction to the basic module. 15. Apparatus as claimed in Claim 11, characterized in that the basic module is arranged with its axis going through the center of the tank and the additive modules are arranged symmetrically and perpendicularly to the basic module. 16. Apparatus as claimed in Claim 15, characterized in that at least one additive module is parallel adjoined to the basic module, the system of parallel modules formed in this way being symmetrical to the axis going through the center of the tank. 17. Apparatus as claimed in Claim 8, characterized in that the aeration elements (3) are in the admission area for the raw waste water arranged with farther spacing than in the next parts of the circulation circuit. 18. Apparatus as claimed in any of the Claims 8 to 17, characterized in that the croεε εectional area of flow of the inlet opening (14) into the fluidized bed filter iε larger than 10% of the surface area in the separation space (4). 19. Apparatus as claimed in Claim 8, characterized in that the collecting equipment is provided with at least one pump, preferably centrifugal pump (36), which is arranged in the collection sump (35). 20. Apparatus as claimed in any of the Claims 8 to 19, characterized in that the separation space (4) for fluidized bed filtration is arranged through the whole length of the channels (5,9) of the circulation circuit, while the inlet of activation mixture into the separation space (4) for fluidized bed filtration and the collecting equipment for carrying the thickened activation mixture out from the separation space (4) are formed through its whole length. 21. Apparatus as claimed in Claim 8, characterized in that a trap (29) for flotated sludge is arranged in the upper part of the separation space (4), said trap (29) being formed by a sloping roof, to the lower side of which a pressure air supply (38) is adjoined, the upper part being provided with a flotated sludge outlet in the form of an air-lift pump (39) mouthing in the activation space, while the whole roof is under the tank surface level. 22. Apparatuε aε claimed in Claim 10, characterized in that at least one flow deflector (20) iε arranged in the area of the paεsage (19) to the partition (2) from the side of the activation space. 23. Apparatus as claimed in Claimε 8 and 22, characterized in that a mixer (46) iε arranged at the beginning of the activation space and the outlet (43) from the pump (41) mouths in the mixer (46), in which admission (22) for raw waste water mouths and the outlet from the mixer (46) mouths in the following part of the activation space. 24. Apparatus as claimed in Claim 10, characterized in that the pump aggregate (41) is a pump provided with a submersible reversing electric motor (42). 25. Apparatus as claimed in Claim 24, characterized in that the reversing electric motor (42) and the runner of the pump (41) are arranged slidingly on guiding bars, located vertically to the tank bottom. 26. Apparatus as claimed in Claim 24, characterized in that the pump (41)is connected with at leaεt two branches of the collecting main (13) . 27. Apparatus as claimed in Claim 10, characterized in that the aeration hoses (47) are located in the activation space and are connected with the pressure air supply through a closing (45) or through a regulator. 28. Apparatus as claimed in Claim 27, characterized in that the aeration hoses (47) are arranged in two branches which are located mutually at the opposite sides of the cross-section of the circumferential channel (7).

Inventors: MACKRLE SVATOPLUK, MACKRLE VLADIMIR, MACKRLE, SVATOPLUK, MACKRLE, VLADIMIR
Applicants: MACKRLE SVATOPLUK, MACKRLE VLADIMIR, MACKRLE, SVATOPLUK, MACKRLE, VLADIMIR
Application year: 1994
Main classification: C02F3
IPC codes: C02F3